Methods and compounds for removing non-acidic contaminants from hydrocarbon streams

ABSTRACT

An extraction solvent comprised of one or more ethyleneamines having structure (I), (II), or (III): 
                         
where R 1 -R 6  can independently be H, C 1 -C 4  linear or branched alkyl, amido (RRNC═O), or hydroxyalkyl, where each R in the amido group independently H or C 1  alkyl, and where x ranges from 1 to 6, may be contacted with a hydrocarbon stream to remove or extract non-acidic contaminants, such as thiophenes, benzothiophenes, alkyl sulfides, alkyl disulfides, mercaptans, aromatics, oxygenates, metals, olefins, and combinations thereof, from the hydrocarbon stream. The extraction solvent may include co-solvents and the hydrocarbon stream may be in gas and/or liquid form.

TECHNICAL FIELD

The present invention relates to methods and compounds for removal ofnon-acidic contaminants from a hydrocarbon stream, and more particularlyrelates, in one non-limiting embodiment, to contacting an extractionsolvent comprising one or more ethyleneamines and derivatives thereofwith a hydrocarbon stream to remove at least a portion of non-acidiccontaminants from the hydrocarbon stream.

BACKGROUND

New domestic regulations and international standards aimed at reducingemissions from the burning of fuels for energy are puttingever-increasing restrictions on the allowable sulfur content of finishedhydrocarbon streams across the global oil & gas industry.

As part of the ongoing initiative to improve ambient air quality, theU.S. Environmental Protection Agency (EPA) in 2017 revised theirgasoline standards around sulfur content from the previous Tier 2specifications to the new Tier 3 specifications. Consequently,refineries are being forced to reduce the total sulfur content in lighthydrocarbons that may be used as blend components in their finishedgasoline or diesel pools. They also have to find new and novel ways tolower the sulfur content in finished fuels that may be off specificationfor sulfur content after processing. Traditional processing technologiesfor sulfur removal from hydrocarbon streams in petroleum refiningindustries mainly include catalytic hydro-desulfurization (HDS orHydrotreater), and/or the use of a combination of mechanical andchemical treatment systems. For example, it is common in refineryprocesses to use caustic soda as part of a caustic treater unit andcertain amines (ethanolamines in particular) as part of an aminescrubber unit.

Designed in alignment with refinery capacity, these technologies areusually capable of processing large volumes and they provide a certainlevel of operation flexibility for constantly changing feedstocksregarding sulfur species and sulfur levels. However, with higherdesulfurization demands on both throughput and sulfur removalefficiency, these processes still leave fundamental gaps in respondingto the sulfur removal needs. For example, while a caustic scrubber isefficient at removing acidic species like H₂S (hydrogen sulfide) andlower molecular weight mercaptans, and an amine unit is efficient atremoving H₂S and acidic CO₂, these processes have very limited impact onany of the non-acidic sulfur compounds that are commonly found inrefinery intermediate and blend streams, such as carbonyl sulfide (COS),dimethyl disulfide (DMDS), dimethyl sulfide (DMS), carbon disulfide(CS₂), thiophenes, as well as, olefins, oxygenates, aromatics andmetals.

Removal of such non-acidic contaminants have been accomplished viamethods such as extractive distillation or a liquid-liquid extraction.As shown in the illustration in FIG. 1, in a liquid-liquid extractionprocess 100, a hydrocarbon stream containing non-acidic contaminants 101of the kinds described above is contacted/reacted with an extractionsolvent 102 to extract contaminants from the hydrocarbon stream into thesolvent and separate the two liquids into a hydrocarbon stream with areduced amount of non-acidic contaminants 103 and an extraction solventstream laden with non-acidic contaminants 104. Separation of the liquidsafter contact is critical to the efficacy of the extraction process.Therefore, not only must a contaminant and/or its reaction adduct besoluble in the extraction solvent, the contaminant-laden solvent must beimmiscible in the hydrocarbon stream being treated.

Some extraction solvents commonly used in liquid-liquid extractionsinclude sulfolanes, pyrrolidones, glycols, carbonates, morpholine,furfural, alcohols and hydroxylamines. While these chemistries have beenshown to provide marginal sulfur-contaminant reduction across a widerarray of sulfur compounds compared to traditional refinery processes,they have also been found to be completely soluble in the hydrocarbonstream and have resulted in little or no separation of the hydrocarbonstream from the contaminant-laden extraction stream.

Therefore, a need still exists for an extraction solvent having improvedextraction efficacy to meet the more stringent sulfur limits forhydrocarbon streams that have been set by the EPA and other regulatorybodies.

SUMMARY

There is provided, in one form, a process for removal of non-acidiccontaminants from a hydrocarbon stream comprising the contaminants inwhich the hydrocarbon stream containing non-acidic contaminants iscontacted with an extraction solvent comprising one or moreethyleneamines having structure (I), (II), or (III):

where R₁-R₆ can independently be H, C₁-C₄ linear or branched alkyl,amido (RRNC═O), or hydroxyalkyl, where each R in the amido group isindependently H or C₁ alkyl, and where x ranges from 1 to 6. In onenon-limiting embodiment, the non-acidic contaminants are of thiophenes,benzothiophenes, alkyl sulfides, disulfides, mercaptans, aromatics,oxygenates, metals, and/or olefins.

There is further provided in another form, a treated fluid comprising,in a ratio ranging from about 1:10 to about 95:100, a liquid or gashydrocarbon stream containing non-acidic contaminants and an extractionsolvent comprising one or more ethyleneamines having structure (I),(II), or (III):

where R₁-R₆ can independently be H, C₁-C₄ linear or branched alkyl,amido (RRNC═O), or hydroxyalkyl, where each R in the amido group isindependently H or C₁ alkyl, and where x ranges from 1 to 6.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic illustration of a liquid-liquid extraction processfor removing non-acidic contaminants from a liquid hydrocarbon streamusing an extraction solvent.

DETAILED DESCRIPTION

It has been discovered that contacting a hydrocarbon stream containingnon-acidic contaminants with an effective amount of an extractionsolvent comprising ethyleneamines of a certain structure is useful oreffective for removing the non-acidic contaminants from the hydrocarbonstream.

In one embodiment, the extraction solvent useful for contaminant removalmay comprise one or more ethyleneamines having the following generalstructure:R₁R₂N(R₃NR₄)NR₅R₆  (I)where R₁-R₆ can independently be H, C₁-C₄ linear or branched alkyl,amido (RRNC═O), or hydroxyalkyl, and where each R in the amido group isindependently H or C₁ alkyl. Non-exclusive examples of useful andeffective extraction solvents falling under this formula arediethylenediamine, diethylenetriamine (DETA), and triethylenetriamine(TETA).

In another non-limiting embodiment, the one or more ethyleneamines to beused in the extraction solvent may have the following structure (II):

where R₁-R₄ can independently be H, C₁-C₄ linear or branched alkyl,amido (RRNC═O), or hydroxyalkyl, and where each R in the amido group isindependently H or C₁ alkyl.

The one or more ethyleneamines may also have the following structure(III):

where R-R₅ can independently be H, C₁-C₄ linear or branched alkyl, amido(RRNC═O), or hydroxyalkyl, where each R in the amido group isindependently H or C₁ alkyl, and where x ranges from 1 to 6.

It is understood that the choice of R groups is made with the goal ofoptimizing the immiscibility or insolubility of the extraction solventwith hydrocarbon stream being treated in order to facilitate separationof the contaminant-laden extractive solvent stream from the hydrocarbonstream after they are contacted or mixed.

The extraction solvent may further comprise a co-solvent that iscompatible with the one or more ethyleneamines described above and thatis substantially insoluble in the hydrocarbon stream. Non-limitingexamples of co-solvents that may meet this criteria include, but are notlimited to, water, alcohols, glycols, amides, ester, amines, quaternaryammonium compounds, carbonates, ketones and combinations thereof.

The hydrocarbon stream to be treated with an extraction solventcomprised of one or more ethyleneamines of the kinds described above maybe any industrial hydrocarbon stream, in liquid and/or gas form, thatcontains non-acidic contaminants. Such streams include, but are notlimited to, refinery feedstock, particularly light petroleum gases(LPG), such as (iso)butane and (iso)propane, straight run distillates,cracked stocks, hydrotreated materials, and/or finished fuel blends. Thehydrocarbon stream may contain from about 1 ppm to about 10,000 ppm ofwater, more typically from about 50 ppm to about 1,000 ppm of water.

The removal of the non-acidic contaminants from the hydrocarbon streamusing the extraction solvent of the kind described herein may beaccomplished, in one non-limiting embodiment, by the liquid-liquidextraction process shown in FIG. 1 in which the hydrocarbon streamcontaining non-acidic contaminants 101 is contacted/reacted/mixed withthe extraction solvent 102 to extract the non-acidic contaminants fromthe hydrocarbon stream into the solvent and form two separate liquidphases: a hydrocarbon stream with a reduced amount of non-acidiccontaminants 103 and an extraction solvent stream laden with non-acidiccontaminants 104. In a non-limiting embodiment, the extraction processmay have a counter-flow design, meaning that the hydrocarbon streamcontaining the non-acidic contaminants and the extraction solvent streamflow in opposite directions from one another prior to and while beingcontacted/mixed/reacted. In yet another non-limiting embodiment, thecontacting of the hydrocarbon stream and the extraction solvent isachieved by injecting the extraction solvent directly into thehydrocarbon stream.

In a further process step, the contaminant-laden extraction solventstream may be separated from the hydrocarbon stream having a reducedamount of non-acidic contaminants using a knockout drum, a centrifuge,and/or an absorbent material and the separated contaminant-ladenextraction solvent stream may be regenerated by passing thecontaminant-laden extraction solvent stream through selective filtrationmedia or more adsorption material to remove the contaminants.

The non-acidic contaminants present in the hydrocarbon stream may besulfur compounds, such as, without limitation, thiophenes,benzothiophenes, alkyl sulfides, alkyl disulfides, carbonyl sulfide(COS), carbon disulfide (CS₂), and combinations thereof. The non-acidiccontaminants to be removed using the extraction solvent may alsoinclude, without limitation, mercaptans, aromatics, oxygenates, metals,olefins, and combinations thereof. In one non-limiting embodiment,mercaptans that may be removed by this method include, but are notnecessarily limited to, straight chained or branched, primary, secondaryor tertiary mercaptans with a carbon range of C₁-C₅. In anothernon-restrictive version, aromatics, including substituted and fused-ringaromatics that may be removed by this method include, but are notnecessarily limited to, benzene, toluene, naphthalene, and anthracene.In a different non-limiting embodiment, oxygenates that may be removedby this method include, but are not necessarily limited to, straightchained or branched, primary, secondary, tertiary alcohols, and ethers.Further, metals that may be removed by this method include, but are notnecessarily limited to, organics, including iron and chlorine, andinorganics, such as chlorides and FeS. Additionally, olefins that may beremoved by this method include, but are not necessarily limited to,straight chained or branched, mono, di or poly olefins.

In one embodiment, the ratio of the amount of one or more ethyleneaminesto the amount of hydrocarbon in the hydrocarbon stream may range fromabout 1:10 independently to about 95:100 independently, or from about25:100 independently to about 75:100 independently, or may be about50:50. For purposes of this disclosure, the term “independently” withrespect to a range means that any threshold may be used together withany other threshold to form an acceptable alternative range

In another exemplary embodiment, the ratio of the amount of one or moreethyleneamines to the amount of co-solvent in the extraction solvent mayrange from about 100:0.00001 independently to about 25:75 independently,or may be about 90:10.

A goal of the contacting the extraction solvent with the hydrocarbonstream containing non-acidic contaminants is to reduce the amount ofcontaminants to an acceptable environmental level. Complete removal ofthe contaminants from the hydrocarbon stream is desirable, but it shouldbe appreciated that complete removal is not necessary for the methodsand compounds discussed herein to be considered effective. Success isobtained if more contaminants are removed from the hydrocarbon streamusing the extraction solvent described herein than in the absence of aneffective amount of the extraction solvent, and particularly if thecontaminants are reduced to an acceptable environmental level.

The invention will be further described with respect to the followingExamples, which are not meant to limit the invention, but rather tofurther illustrate the various embodiments.

EXAMPLES

In one set of evaluations, samples of model hydrocarbons were preparedby adding known amounts of specific types of sulfur compounds. A mixture40 mL of the model hydrocarbon and 40 mL of the extraction solvent wasagitated for 5 minutes and then centrifuged at 1500 rpm for 15 minutesto separate the oil/water phases. A small sample of the hydrocarbonphase was then taken from the container and analyzed for total sulfurcontent using a XOS Sindie model 2622 10 sulfur analyzer via ASTM D7059.Sulfur reduction, as a percentage, was calculated using the followingequation:[(ppm sulfur in the untreated fuel)−(ppm sulfur in treated fuel)/(ppmsulfur in untreated fuel)]×100

In another set of evaluations, using the same testing method as setforth above, a few “clean” hydrocarbon (pentane, gasoline, kerosene, orultra-low sulfur kerosene (ULSK)) samples were “spiked” with knownamounts of specific sulfur compounds to understand which chemistriesworked best in removing which sulfur compounds. These real field sampleshad a ratio of hydrocarbon to extraction solvent of 1:1.

The results of the evaluations of performance of the various extractionsolvents contacted with the hydrocarbon samples is shown below in Tables1-8. In the Tables, RSH stands for mercaptan, and thiophenes represent amixture of 100 ppm each of tetrahydrothiophene, thiophene, and2-methylthiophene.

The data in these Tables show that, in most instances, TETA and DETA doa better job of removing or reducing the amount of most of the sulfurcompounds in these various hydrocarbon streams than most of the otherextraction solvents tested.

TABLE 1 Comparing Reduction of Certain Sulfur Compounds in ModelHydrocarbons Using Various Extraction Solvents Sulfur Sulfur % SulfurExtraction Solvent Compounds ppm Reduction Blank Dimethylsulfide (DMS)177, 186 — Diethylenetriamine (DETA) Dimethylsulfide (DMS) 76 55%2-Pyrrolidone Dimethylsulfide (DMS) 92 45% Fe dibutylamine 1:1 ratioDimethylsulfide (DMS) 112 38% NaBH4 (20%) + EDA Dimethylsulfide (DMS)113 37% EXALT 1100 + EDA Dimethylsulfide (DMS) 141 22% Methanol/water20/20ml Dimethylsulfide (DMS) 163  9% Y17BH12119 (100 + MeOH)Dimethylsulfide (DMS) 171  8% Y18BH12130 (Quat) Dimethylsulfide (DMS)179  4% 65% EXALT 1100 Dimethylsulfide (DMS) 184  1% EXALT 1100Dimethylsulfide (DMS) 186  0% Blank DMS, DMDS, Ethyl RSH 285, 262, — 2752-Pyrrolidone DMS, DMDS, Ethyl RSH 106 63% Diethylenetriamine (DETA)DMS, DMDS, Ethyl RSH 112.1 61% Triethylentetraamine (TETA) DMS, DMDS,Ethyl RSH 111 60% NaBH4/NMP DMS, DMDS, Ethyl RSH 158 43% NaBH4(6.5%)/DETA DMS, DMDS, Ethyl RSH 151.48 42% Ethylamine DMS, DMDS, EthylRSH 165.7 42% Monoethanolamine (MEA) DMS, DMDS, Ethyl RSH 195.4 31%NaBH4 (17%)/Ethylamine DMS, DMDS, Ethyl RSH 197 28% Quaternary AmmoniumDMS, DMDS, Ethyl RSH 226 21% Hydroxide Caustic/Glycerol/H2O DMS, DMDS,Ethyl RSH 223 19% Quat/2-Pyrrolidone DMS, DMDS, Ethyl RSH 217.67 17%NaBH4 (6.5%)/MEA DMS, DMDS, Ethyl RSH 221.36 16% Caustic DMS, DMDS,Ethyl RSH 0%, 13% Liquid Ammonia DMS, DMDS, Ethyl RSH 264.1  7%Glycerine DMS, DMDS, Ethyl RSH 275.5  3%

TABLE 2 Comparing Reduction of Certain Sulfur Compounds from Gasoline,Pentane, and Kerosene Using Caustic, Pyrrolidone, Quaternary AmmoniumHydroxide, DETA, and TETA % Sulfur Reduction Sulfur Content QuaternaryHydrocarbon Sulfur Blank, Pyrollidone Ammonium Stream Compounds ppm-vCaustic (NMP) Hydroxide DETA TETA Refinery Ethyl Mercaptan 188 23% 57%43%  69% Gasoline Refinery Dimethylsulfide 177, 186 0 45% 4% 55% 70%Gasoline (DMS) Refinery Thiophenes 223  0% 50% 2% 43% 63% GasolineRefinery Carbon 207, 213  4% 42% 8% 88% 83% Gasoline Disulfuide (CS2)Refinery Butyl Mercaptan 114, 117  2% 36% 9% 54% — Gasoline NaturalVarious 468, 448 13% 33% 17%  40% — Gasoline Natural Various 484 30% 37%37%  39% — Gasoline Pentane Dimethylsulfide 89  0% 53% 4% 54% — (DMS)Pentane Dimethyldisulfide 133  0% 59% 6% 57% — (DMDS) Pentane CS2 227 0% 30% 3% 99% — Pentane Ethyl Mercaptan 59 99% 55% 99%  63% — PentaneButyl Mercaptan 53 66% 32% 99%  54% — Pentane DMS, DMDS, 49 20% 65% 76%CS2, Ethyl RSH Kerosene Dimethylsulfide 55.5 12% 58% 15%  89% 65% (DMS)Kerosene Dimethyldisulfide 91.6  1% 59% 3% 69% 62% (DMDS) Kerosene CS2128.79  3% 44% 7% 99% 65% Kerosene Ethyl Mercaptan 53.4 93% 55% 93%  67%— Kerosene Thiophenes 140.59  1% 56% 3% 67% 68% Kerosene Various 454.712% 51% 17%  70% —

TABLE 3 Comparing Reduction of Thiophenes from Refinery B Gasoline UsingVarious Extraction Solvents Sulfur Sulfur Content, % Sulfur SampleCompounds ppm Reduction Refinery B Gasoline Blank Thiophenes 223 —Refinery B Gasoline w/Na 228 0% Borohydride Refinery B w/50% Na 216 3%Borohydride (in Methanol) Refinery B Gasoline w/Quaternary 219 2%Ammonium Hydroxide Refinery B Gasoline w/DETA 120 43%  Refinery BGasoline w/2- 79 65%  Pyrollidone

TABLE 4 Comparing Reduction of Various Sulfur Compounds from Refinery MULSK Using Various Extraction Solvents Sulfur Sulfur Content, % SulfurSample Compounds ppm Reduction Refinery M ULSK Baseline Various 675 —Refinery M ULSK w/50% Na compounds 670  1% Borohydride Refinery M ULSKw/Quaternary 664 2.0%  Ammonium Hydroxide Refinery M ULSK w/90/10 32752% NMP/H2O Refinery M ULSK w/DETA 320 52%

TABLE 5 Comparing Reduction of Benzothiophenes and Dibenzothiophenesfrom Refinery A Diesel Using Various Extraction Solvents Sulfur SulfurContent, % Sulfur Sample Compounds ppm Reduction Refinery A DieselBaseline Benzothiophenes, 249.48 — Refinery A Diesel w/50%Dibenzothiophenes 246.79  1% Na Borohydride Refinery A Diesel w/ 244.23 2% Quaternary Ammonium Hydroxide Refinery A Diesel w/90/ 197.16 21% 10NMP/H2O Refinery A Diesel w/DETA 204.94 18%

TABLE 6 Comparing Reduction of Various Sulfur Compounds from Terminal CNatural Gas Using Various Extraction Solvents Sulfur Sulfur Content, %Sulfur Sample Compounds ppm Reduction Terminal C Natural Gas BaselineVarious 139.28 — Terminal C Natural Gas w/50% Na compounds 118 16%Borohydride Terminal C Natural Gas w/50% Na 117 15% Borohydride (Buyout)Terminal C Natural Gas w/ 98.77 29% Quaternary Ammonium HydroxideTerminal C Natural Gas w/90/10 84.98 39% NMP/H2O Terminal C Natural Gasw/DETA 79.76 43%

TABLE 7 Comparing Reduction of Various Sulfur Compounds from Terminal CCat Naphtha Using Various Extraction Solvents Sulfur Sulfur Content, %Sulfur Sample Compounds ppm Reduction Terminal C Cat Naphtha BaselineVarious 222 — Terminal C Cat Naphtha w/50% compounds 209  6% NaBorohydride Terminal C Cat Naphtha w/ 204  8% Quaternary AmmoniumHydroxide Terminal C Cat Naphtha w/ 104 53% 90/10 NMP/H2O Terminal C CatNaphtha w/ 109 51% DETA

TABLE 8 Comparing Reduction of Various Sulfur Compounds from Terminal PGasoline Using Various Extraction Solvents Sulfur Sulfur Content, %Sulfur Sample Compounds ppm Reduction Terminal P Gasoline BaselineThiophenes, 448 — Terminal P Gasoline w/50% Diethyl Sulfides, 367 18 NaBorohydride (In Methanol) Isopropyl RSH, Terminal P Gasoline w/ MethylEthyl 370 17 Quaternary Ammonium RSH, Dimethyl Hydroxide Disulfides,Terminal P Gasoline with Isobutyl RSH 376 16 65% Na Borohydride (inwater) Terminal P Gasoline w/Na 389 13 Borohydride Terminal P GasolineBlank 468 — Retest Terminal P Gasoline w/DETA 289, 279 40 Terminal PGasoline w/2- 294 37 Pyrrolidone

In the foregoing specification, the invention has been described withreference to specific embodiments thereof. However, the specification isto be regarded in an illustrative rather than a restrictive sense. Forexample, hydrocarbon streams, ethyleneamines, co-solvents, contaminants,contact/extraction processes, and separation mechanisms falling withinthe claimed or disclosed parameters, but not specifically identified ortried in a particular example, are expected to be within the scope ofthis invention.

The present invention may be practiced in the absence of an element notdisclosed. In addition, the present invention may suitably comprise,consist or consist essentially of the elements disclosed. For instance,the process may comprise, consist of, or consist essentially ofcontacting a hydrocarbon stream containing non-acidic contaminants withan extraction solvent consisting essentially of or consisting of one ormore ethyleneamines having structure (I), (II), or (III):

where R₁-R₆ can independently be H, C₁-C₄ linear or branched alkyl,amido (RRNC═O), or hydroxyalkyl, where each R in the amido group isindependently H or C₁ alkyl, and where x ranges from 1 to 6.

Alternatively, the treated fluid may comprise, consist of, or consistessentially of a hydrocarbon stream containing non-acidic contaminants;and an extraction solvent consisting of or consisting essentially of oneor more ethyleneamines having structure (I), (II), or (III):

where R-R₆ can independently be H, C₁-C₄ linear or branched alkyl, amido(RRNC═O), or hydroxyalkyl, where each R in the amido group isindependently H or C₁ alkyl, and where x ranges from 1 to 6.

The words “comprising” and “comprises” as used throughout the claims,are to be interpreted to mean “including but not limited to” and“includes but not limited to”, respectively.

As used herein, the word “substantially” shall mean “being largely butnot wholly that which is specified.”

As used herein, the singular forms “a,” “an,” and “the” are intended toinclude the plural forms as well, unless the context clearly indicatesotherwise.

As used herein, the term “about” in reference to a given parameter isinclusive of the stated value and has the meaning dictated by thecontext (e.g., it includes the degree of error associated withmeasurement of the given parameter).

As used herein, the term “and/or” includes any and all combinations ofone or more of the associated listed items.

What is claim is:
 1. A process for removal of non-acidic contaminantsfrom a hydrocarbon stream comprising the contaminants, the processcomprising: contacting the hydrocarbon stream containing non-acidiccontaminants selected from a group consisting of thiophenes,benzothiophenes, alkyl sulfides, alkyl disulfides, mercaptans,aromatics, oxygenates, metals, olefins, and combinations thereof with anextraction solvent comprising one or more ethyleneamines havingstructure (I), (II), or (III):

where R₁ is H, R₂-R₆ is, to the extent chemically possible,independently H, C₁-C₄ linear or branched alkyl, amido (RRNC═O), orhydroxyalkyl, where each R in the amido group is independently H or C₁alkyl, and where x ranges from 1 to 6; and upon contacting thehydrocarbon stream with the extraction solvent, a portion of thenon-acidic contaminants are removed from the hydrocarbon stream.
 2. Theprocess of claim 1, wherein the ratio of the one or more ethyleneaminesto hydrocarbon in the hydrocarbon stream ranges from about 1:10 to about95:100.
 3. The process of claim 1, wherein the extraction solventcomprises triethylenetriamine or diethylenetriamine.
 4. The process ofclaim 1, wherein the extraction solvent further comprises a co-solventselected from a group consisting of water, an alcohol, a glycol, anamide, an ester, an amine different from the ethyleneamine, a quaternaryammonium compound, and combinations thereof.
 5. The process of claim 1,wherein the hydrocarbon stream is selected from the group consisting ofa gas stream, a liquid stream, and combinations thereof.
 6. The processof claim 1, wherein the contacting is achieved by an extraction processhaving a counter-flow design between the hydrocarbon stream and theextraction solvent.
 7. The process of claim 1, wherein the contacting isachieved by injecting the extraction solvent directly into thehydrocarbon stream.
 8. The process claim 1, further comprising creatingan immiscible two-phase liquid comprising a contaminant-laden extractionsolvent stream and a hydrocarbon stream having a reduced amount ofnon-acidic contaminants after the hydrocarbon stream is contacted withthe extraction solvent.
 9. The process of claim 8, wherein thecontaminant-laden extraction solvent stream is separated from thehydrocarbon stream having a reduced amount of non-acidic contaminantsusing a separation mechanism selected from the group consisting of aknockout drum, a centrifuge, an absorbent material, and combinationsthereof thereby giving a separated contaminant-laden extraction solventstream.
 10. The process of claim 9, further comprising regenerating theseparated contaminant-laden extraction solvent stream by passing thecontaminant-laden extraction solvent stream through selective filtrationmedia or additional adsorption material thereby removing thecontaminants.